A fluidized bed reactor, a device, and a method for producing low-carbon olefins from oxygen-containing compound are provided. The fluidized bed reactor includes a reactor shell, a reaction zone, a coke control zone and a delivery pipe, where there are n baffles arranged in the coke control zone, and the n baffles divide the coke control zone into n sub-coke control zones which include a first sub-coke control zone, a second sub-coke control zone, and an nth sub-coke control zone; at least one catalyst circulation hole is provided on each of the n-1 baffles, so that the catalyst flows in an annular shape in the coke control zone, where n is an integer. The device and method can be adapted to a new generation of DMTO catalyst, and the unit consumption of production ranges from 2.50 to 2.58 tons of methanol/ton of low-carbon olefins.

The present invention relates to a method of subjecting a biomass feedstock to hydropyrolysis, the method at least comprising the steps of: a) supplying a biomass feedstock and a fluidizing gas comprising hydrogen to a bulk reactor zone of a fluidized bed reactor containing a deoxygenating catalyst; b) subjecting the biomass feedstock in the bulk reactor zone of the fluidized bed reactor to a hydropyrolysis reaction by contacting the biomass feedstock with the deoxygenating catalyst in the presence of the fluidizing gas, thereby obtaining a hydropyrolysis reactor output comprising at least one non-condensable gas, a partially deoxygenated hydropyrolysis product and char; wherein the bulk reactor zone is cooled by means of a cooling fluid flowing through a plurality of tubes running through the bulk reactor zone, the plurality of tubes having inlets into and outlets from the bulk reactor zone; and wherein the cooling fluid flowing in the tubes at the point (‘A’) where the biomass feedstock enters the bulk reactor zone has a temperature of at least 320° C., preferably at least 340° C., more preferably at least 350° C., even more preferably at least 370° C., yet even more preferably at least 380° C.

Systems and methods are provided for increasing the yield of products generated during co-processing of biomass oil in a fluid catalytic cracking (FCC) system. The systems and methods can allow for increased yield by reducing or minimizing formation of carbon oxides, gas phase products, and/or coke yields during the co-processing. This can be achieved by adding a hydrogen-rich co-feed to the co-processing environment. Examples of hydrogen-rich co-feeds include high hydrogen content vacuum gas oil co-feed, high hydrogen content distillate co-feed, and/or high hydrogen content naphtha co-feed. Additionally or alternately, various types of fractions that contain a sufficient amount of hydrogen donor compounds can be used to reduce or minimize carbon oxide formation

A method may include: providing bio waste stream wherein the bio waste stream comprises at least one bio waste selected from the group consisting of palm oil mill effluent, soapstock, and combinations thereof; introducing the bio waste effluent stream into a fluidized catalytic cracking unit; contacting the bio waste with a catalyst in the fluidized catalytic cacking unit; and cracking at least a portion of the bio waste stream to form cracked products that comprise a cracked product stream.

A method for preparing a high-quality fuel oil and/or chemical raw material from a biomass pyrolysis liquid. In the method, a biomass pyrolysis liquid undergoes a hydrodeoxygenation reaction in a catalyst full mixing flow circulation system in a fluidized bed reactor to obtain deoxygenated oil, and the obtained deoxygenated oil undergoes a hydrocracking reaction in a fixed bed reactor to obtain high-quality fuel oil and/or a chemical raw material. The method may prevent the condensation and coking of a biomass pyrolysis liquid, solve the problem of rapid catalyst deactivation, and may convert a biomass pyrolysis liquid into a high-quality fuel oil that may be directly used by vehicles and into a chemical product.

The present disclosure relates to an FCC catalyst composition and a process for preparing the same. In a first aspect, there is provided an FCC catalyst composition comprising 25 to 45 wt % Y-type zeolite, 20 to 40 wt % silicon oxide, 5 to 25 wt % alumina, 5 to 35 wt % of at least one clay and 0.5 to 3 wt % of at least one rare earth oxide. The weight % of each of the component is with respect to the total weight of the composition. The FCC catalyst composition has an average particle size in the range of 45-120μ. In a second aspect, there is provided a process for preparing the FCC catalyst composition, which uses ball milled pseudoboehmite having an average particle size in the range of 1 to 8 micron and the whole process is carried out at a pH value in the range of 6 to 7.

A system for producing catalytically treated pyrolytic vapor.The system comprises a pyrolysis reactor (100) configured to produce pyrolytic vapor and a catalytic reactor (200) limiting abed area (B) into which a fluidized catalyst bed is configured to form in use. The catalytic reactor (200) comprises a static mixer (300) configured to spread the particulate catalyst within the bed area (B). Thus, the catalytic reactor (200) is configured to produce a mixture of the particulate catalyst and the catalytically treated pyrolytic vapor from the pyrolytic vapor. A method for producing catalytically treated pyrolytic vapor. The method comprises producing pyrolytic vapor and allowing at least a clean part of the pyrolytic vapor to chemically react in the presence of the particulate catalyst to produce a mixture of the particulate catalyst and catalytically treated pyrolytic vapor. The method comprises mixing, in the bed area, the pyrolytic vapor and the particulate catalyst with a static mixer.

A process is provided for the catalytic cracking of a glyceride oil feedstock with a catalyst composition containing a deactivated phosphorus-containing ZSM-5 light olefins selective additive.

Digestion of cellulosic biomass solids may be complicated by release of lignin therefrom. Methods and systems for processing a reaction product containing lignin-derived products, such as phenolics, can comprise hydrotreating the reaction product to convert the lignin-derived products to desired higher molecular weight compounds. The methods and systems can further include separating the higher molecular weight compounds from unconverted products, such as unconverted phenolics, and recycling the unconverted phenolics for use as at least a portion of the digestion solvent and for further conversion to desired higher molecular weight compounds with additional hydrotreatment. The methods and systems can further include a further hydrotreatment step configured for additional lignin conversion and/or a further hydrotreatment step configured for generating hydrogen.

Digestion of cellulosic biomass solids may be complicated by release of lignin therefrom. Methods and systems for processing a reaction product containing lignin-derived products, such as phenolics, can comprise hydrotreating the reaction product to convert the lignin-derived products to desired higher molecular weight compounds. The methods can further include separating the higher molecular weight compounds from unconverted products, such as unconverted phenolics, and recycling the unconverted phenolics for use as at least a portion of the digestion solvent and for further conversion to desired higher molecular weight compounds with additional hydrotreatment. The methods and systems can further include generating hydrogen with the further hydrotreatment.